Method and system for performing thermochemical conversion of a carbonaceous feedstock to a reaction product

ABSTRACT

The thermochemical conversion of biomass material to one or more reaction products includes generating thermal energy with at least one heat source, providing a volume of feedstock, providing a volume of supercritical fluid, transferring a portion of the generated thermal energy to the volume of supercritical fluid, transferring at least a portion of the generated thermal energy from the volume of supercritical fluid to the volume of feedstock, and performing a thermal decomposition process on the volume of feedstock with the thermal energy transferred from the volume of supercritical fluid to the volume of the feedstock in order to form at least one reaction product.

CROSS-REFERENCE TO RELATED APPLICATION

The present application is related to and claims the benefit of theearliest available effective filing date(s) from the following listedapplication(s) (the “Related Applications”) (e.g., claims earliestavailable priority dates for other than provisional patent applicationsor claims benefits under 35 USC §119(e) for provisional patentapplications, for any and all parent, grandparent, great-grandparent,etc. applications of the Related Application(s)).

RELATED APPLICATIONS

-   -   For purposes of the USPTO extra-statutory requirements, the        present application constitutes a regular (non-provisional)        patent application of United States Provisional Patent        Application entitled SYSTEMS AND METHODS FOR CONVERTING BIOMASS        FEEDSTOCK TO REFINED PRODUCTS, naming JOSHUA C. WALTER and        MANUEL GARCIA-PEREZ as inventors, filed Mar. 15, 2013,        Application Ser. No. 61/794,121.

TECHNICAL FIELD

The present disclosure generally relates to the thermochemicalconversion of a carbonaceous feedstock to a reaction product, and inparticular, the thermochemical decomposition of the carbonaceousfeedstock to a reaction product using thermal energy transferred from aselected heat source via a supercritical fluid thermally coupling thefeedstock and a selected heat source.

BACKGROUND

Hydrothermal liquefaction is a process commonly used for the productionof crude bio-oils from lignocellulosic materials and algae. Inhydrothermal liquefaction, the thermochemical reactions generally occurin an aqueous environment at temperatures above 250° C. and pressures ofapproximately 3000 psi for approximately 2-3 hours. The oil produced viahydrothermal liquefaction is primarily formed by products of lignindepolymerization reactions. The products from cellulose andhemicelluloses are soluble in water and, as such, are lost in theaqueous phase. If not recovered, the water soluble organic compounds maycontribute to pollution. Separation of the bio-oil from water generallyinvolves distillation, which is an energy-intensive process. It is,therefore, desirable to provide a process and system that remedy thedefects of the previously known methods.

SUMMARY

In one illustrative embodiment, an method includes, but is not limitedto, generating thermal energy with at least one heat source; providing avolume of feedstock; providing a volume of supercritical fluid;transferring a portion of the generated thermal energy to the volume ofsupercritical fluid; transferring at least a portion of the generatedthermal energy from the volume of supercritical fluid to the volume offeedstock; and performing a thermal decomposition process on the volumeof feedstock with the thermal energy transferred from the volume ofsupercritical fluid to the volume of the feedstock in order to form atleast one reaction product.

In one illustrative embodiment, an apparatus includes, but is notlimited to, a thermochemical conversion system including at least onethermochemical reaction chamber for containing a volume of feedstock;and a thermal energy transfer system including a heat transfer elementcontaining a volume of supercritical fluid in thermal communication withat least one heat source, the thermal energy transfer system arranged toselectably place the volume of supercritical fluid in thermalcommunication with at least a portion of the volume of feedstockcontained within the at least one thermochemical reaction chamber inorder to selectably transfer thermal energy from the at least one heatsource to the at least a portion of the volume of feedstock containedwithin the at least one thermochemical reaction chamber, the at leastone thermochemical reaction chamber configured to thermochemicallyconvert at least a portion of the feedstock to at least one reactionproduct with the thermal energy transferred from the supercriticalfluid.

In one illustrative embodiment, a system includes, but is not limitedto, at least one heat source; a thermochemical conversion systemincluding at least one thermochemical reaction chamber for containing avolume of feedstock; and a thermal energy transfer system including aheat transfer element containing a volume of supercritical fluid inthermal communication with at least one heat source, the thermal energytransfer system arranged to selectably place the volume of supercriticalfluid in thermal communication with at least a portion of the volume offeedstock contained within the at least one thermochemical reactionchamber in order to selectably transfer thermal energy from the at leastone heat source to the at least a portion of the volume of feedstockcontained within the at least one thermochemical reaction chamber.

In addition to the foregoing, various other method and/or system and/orapparatus aspects are set forth and described in the teachings such astext (e.g., claims and/or detailed description) and/or drawings of thepresent disclosure.

The foregoing is a summary and thus may contain simplifications,generalizations, inclusions, and/or omissions of detail; consequently,those skilled in the art will appreciate that the summary isillustrative only and is NOT intended to be in any way limiting. Otheraspects, features, and advantages of the devices and/or processes and/orother subject matter described herein will become apparent in theteachings set forth herein.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1A is a block diagram view of a system for performingthermochemical conversion of a carbonaceous feedstock to a reactionproduct, in accordance with an illustrative embodiment;

FIG. 1B is a block diagram view of a system for performingthermochemical conversion of a carbonaceous feedstock to a reactionproduct, in accordance with an illustrative embodiment;

FIG. 1C is a block diagram view of a system for performingthermochemical conversion of a carbonaceous feedstock to a reactionproduct, in accordance with an illustrative embodiment;

FIG. 1D is a block diagram view of a system for performingthermochemical conversion of a carbonaceous feedstock to a reactionproduct, in accordance with an illustrative embodiment;

FIG. 1E is a block diagram view of a system for performingthermochemical conversion of a carbonaceous feedstock to a reactionproduct, in accordance with an illustrative embodiment;

FIG. 2 is a high-level flowchart of a method for performingthermochemical conversion of a carbonaceous feedstock to a reactionproduct;

FIGS. 3 through 15E are high-level flowcharts depicting alternateimplementations of FIG. 2.

DETAILED DESCRIPTION

In the following detailed description, reference is made to theaccompanying drawings, which form a part hereof. In the drawings,similar symbols typically identify similar components, unless contextdictates otherwise. The illustrative embodiments described in thedetailed description, drawings, and claims are not meant to be limiting.Other embodiments may be utilized, and other changes may be made,without departing from the spirit or scope of the subject matterpresented here.

Referring generally to FIGS. 1A through 1E, a system 100 for performingthermochemical conversion of a feedstock to a reaction product isdescribed.

FIGS. 1A and 1B illustrate a block diagram view of a system 100 forconverting carbonaceous material to one or more reaction products. Inone embodiment, the system 100 includes a thermochemical conversionsystem 102. In one embodiment, the thermochemical conversion system 102includes a thermochemical reaction chamber 104, such as a pyrolysisreaction chamber, suitable for containing a volume of feedstock material105 (e.g., carbonaceous material) and converting the feedstock materialto one or more reaction products, such as, but not limited to, gas, oilor tar.

In another embodiment, the system 100 includes one or more heat sources108. In another embodiment, the system 100 includes a thermal energytransfer system 106 for transferring thermal energy from the one or moreheat sources 108 to the volume of feedstock 105 contained within thethermochemical reaction chamber 104. In one embodiment, the thermalenergy transfer system 106 includes a heat transfer element 107containing a volume of supercritical fluid in thermal communication(e.g., direct or indirect thermal communication) with the one or moreheat sources. For example, the heat transfer element 107 may include,but is not limited to, a heat transfer loop, a heat transfer line andthe like. For instance, the heat transfer element 107 may include, butis not limited to, a heat transfer loop filled with a supercriticalfluid (e.g., super critical carbon dioxide) placed in thermalcommunication (e.g., directly or indirectly) with one or more portionsof the one or more heat sources 108.

In one embodiment, the thermal energy transfer system is arranged toselectably place the volume of the supercritical fluid in thermalcommunication with the volume of feedstock contained within thethermochemical reaction chamber. In this regard, the thermal energytransfer system 106 may selectably transfer thermal energy from the oneor more heat sources 108 to the volume of feedstock 105 contained withinthe at least one thermochemical reaction chamber 104. In anotherembodiment, the thermochemical reaction chamber 104 may thermochemicallyconvert (e.g., convert via pyrolysis, convert via liquefaction or thelike) at least a portion of the feedstock 105 to one or more reactionproducts using the thermal energy carried to the feedstock via thesupercritical fluid.

The supercritical fluid of system 100 may include any supercriticalfluid known in the art suitable for transferring energy from the one ormore heat sources 108 to the feedstock 105 contained in thethermochemical reaction chamber 104. In one embodiment, thesupercritical fluid includes, but is not limited to, supercriticalcarbon dioxide. In another embodiment, the supercritical fluid includes,but is not limited to, water, methanol, ethanol, propanol, acetone. Inanother embodiment, the supercritical fluid is pressurized to highpressure within at least one of the heat transfer element 107 and thethermochemical reaction chamber 104.

It is noted herein that the supercritical fluid of system 100, such as,but not limited to CO₂, may have low viscosity and surface tension,allowing such supercritical fluids to readily penetrate organicmaterials (e.g., biomass material). The penetration of the supercriticalfluid into the feedstock 105 reduces the need for converting thefeedstock 105 into fine particles prior to thermochemical reaction,thereby saving energy in the reaction of the feedstock material. In oneembodiment, in case where the supercritical fluid is supercritical CO₂,the supercritical fluid may be pressurized to above its criticalpressure (72.9 atm) and critical temperature (304 K). It is noted hereinthat above these conditions, CO₂, will display unique solvencyproperties, similar to organic solvents such as hexane, methanol andethanol. The non-polar nature of supercritical CO₂ may facilitate thecontrol of undesirable ionic secondary reactions that commonly occur inaqueous environments. Further, CO₂ will volatize when the system isdepressurized below the critical conditions, which facilitates therecovery of oil with low content of water. Again, this may significantlyreduce energy consumption during reaction product-supercritical fluidseparation, described further herein, following liquefaction and/orpyrolysis. It is further noted herein that liquefaction implement viathe supercritical fluid of system 100 applies heated and pressurized CO₂to the feedstock material 105, which provides for better control ofreaction conditions (e.g., time, pressure, and temperature), therebyallowing for better selectivity of high-value targeted chemicalcompounds or fuel intermediates.

In another embodiment, a supercritical fluid, such as supercritical CO₂,may provide strong temperature and reaction time control via theinjection of cooler supercritical fluid into the thermochemical reactionchamber 104 to quench the reaction or hotter supercritical fluid toaccelerate the reaction. It is further recognized that since a number ofsupercritical fluids, such as supercritical CO₂, can be efficientlycompressed, pressure conditions within the thermochemical reactionchamber 104 may also be used to control thermochemical reactions withinthe thermochemical reaction chamber 104.

It is further noted herein that the supercritical fluid may be utilizedto dry the feedstock 105 prior to liquefaction and/or pyrolysis. Forexample, in the case where the supercritical fluid is sCO₂, prior toliquefaction and/or pyrolysis, the supercritical fluid may serve to drythe feedstock material 105 to remove excess water and impurities. It isfurther noted herein that the drying of the feedstock may reduce theamount of hydrogen needed for hydrotreating and/or hydrocracking the oneor more reaction products.

In another embodiment, the solubility of one or more reaction products,such as bio-oil, in the supercritical fluid are controlled by adding orremoving a polar material into the supercritical fluid. For example, thesolubility of one or more oils in supercritical carbon dioxide may becontrolled by the addition/removal of one or more materials including apolar molecule, such as, but not limited to, H₂, H₂O, an alcohol and thelike. By way of another example, in the case where the feedstockmaterial includes coal, the solubility of one or more oils insupercritical CO₂ may be controlled by adding/removing one or morematerials including a hydrogen donor molecule, such as, but is notlimited to, H₂, H₂O and any other hydrogen donor solvents known in theart.

It is recognized herein that feedstock 105 contained within thethermochemical reaction chamber 104 may include sufficient moisture andpolar nature to adequately dissolve the one or more reaction products(e.g., bio-oil) in the supercritical fluid. As discussed further herein,the ‘dryness’ of the feedstock may be controlled by the thermochemicalconversion system 102 (e.g., controlled via dryer 134), allowing thethermochemical conversion system 102 to maintain a moisture contentlevel within the feedstock 105 to a level sufficient for adequatelydissolving one or more reaction products in the supercritical fluid.

In another embodiment, the supercritical fluid may contain one or morematerials for enhancing one or more physical or thermochemical reactionsin the system 100. For example, the supercritical fluid may contain oneor more catalysts, such as, but not limited to, metals, metal salts andorganics. By way of another example, the supercritical fluid may containone or more solutes, such as, but not limited to, alcohols, oils,hydrogen and hydrocarbons.

The one or more heat sources 108 may include any heat source known inthe art suitable for providing thermal energy sufficient to heat thefeedstock 105 to the selected temperature (e.g., temperature adequatefor fast pyrolysis (e.g., 350-600° C.).

In one embodiment, the one or more heat sources 108 include a non-CO₂emitting heat source. In one embodiment, the one or more heat sources108 include one or more nuclear reactors. The one or more heat sources108 may include any nuclear reactor known in the art. For example, theone or more heat sources 108 may include a liquid metal cooled nuclearreactor, a molten salt cooled nuclear reactor, a high temperature watercooled nuclear reactor, a gas cooled nuclear reactor and the like. Byway of another example, the one or more heat sources 108 may include apool reactor. By way of another example, the one or more heat sources108 may include a modular reactor.

It is recognized herein that a nuclear reactor may generate temperaturessufficient to carry out pyrolysis (e.g., fast pyrolysis) of feedstock105. For example, a nuclear reactor heat source may generatetemperatures in excess of 350-600° C. In this regard, a nuclear reactormay be used to transfer thermal energy (e.g., at a temperature in excessof 350-600° C.) to the supercritical fluid (e.g., supercritical CO₂). Inturn, the supercritical fluid may transfer the nuclear reactor generatedthermal energy to the feedstock 105 contained within the thermochemicalreaction chamber 104.

It is further noted herein that a nuclear reactor heat source isparticularly advantageous as a heat source in the context of system 100because the thermochemical reaction temperatures of system 100 arewithin the range of operating temperatures for many nuclear reactors.Nuclear reactor heat may be used to create reaction products (e.g.,bio-oil) in the thermochemical reaction chamber 104 at high efficiencysince the nuclear reactor is operating at the reaction temperature forthe thermochemical conversion (i.e., heat added at the thermochemicalreaction temperature supplies the required reaction enthalpy).

In one embodiment, the supercritical fluid of system 100 serves as asafety mechanism in the operation of the nuclear reactor driventhermochemical conversion system 112 of system 100. By way of example,supercritical carbon dioxide may be stored in one or more reservoirs(not shown) or tanks (not shown). It is noted herein that supercriticalcarbon dioxide stored in this in this manner may be used to provide athermal buffer between the reactor and the thermochemical conversionsystem 102 by acting as a thermal dashpot. In another embodiment, thesupercritical fluid may be stored at temperatures and pressures suitablefor discharge into the thermomechanical rotating machinery, such as aturbine. In this manner, a selected amount of work may be developed bythe compressed CO₂ to provide mechanical or electric power to safetysystems, such as flow valves, safety valves, isolation valves, pumps,and the like.

In one embodiment, as shown in FIG. 1A, the thermal energy transfersystem 106 includes a direct heat exchange system configured to transferthermal energy directly from the one or more heat sources 108 to thevolume of the supercritical fluid of the heat transfer element 107. Forexample, the heat transfer element 107 may be placed in direct thermalcommunication with a portion of the one or more heat sources 108. Forinstance, in the case where the one or more heat sources 108 includes anuclear reactor, one or more coolant systems of the nuclear reactor maybe integrated with the thermal energy transfer system 106. In thisregard, the nuclear reactor may utilize a supercritical fluid in one ormore coolant systems, which may then be coupled directly to thethermochemical reaction chamber 104. For example, a primary orintermediate coolant loop of the nuclear reactor may include a coolantfluid consisting of a supercritical fluid, such as supercritical CO₂.Further, the coolant loop of the nuclear reactor may be directly coupledto the thermochemical reaction chamber 104 via the thermal energytransfer system 106 so as to intermix the supercritical fluid of thecoolant loop of the nuclear reactor with the feedstock material 105contained within the thermochemical reaction chamber 104. In turn, upontransferring thermal energy from the nuclear reactor to the feedstockmaterial 105, the thermal energy transfer system 106 may circulate thesupercritical fluid coolant back to the nuclear reactor via return path118. It is further contemplated herein that the thermal energy transfersystem 106 may include any number of filtration elements in order toavoid transfer of feedstock and/or reaction products to the coolantsystem(s) of the nuclear reactor.

In another embodiment, as shown in FIG. 1B, the thermal energy transfersystem 106 includes an indirect heat exchange system. In one embodiment,the indirect heat exchange system is configured to indirectly transferthermal energy from the one or more heat sources 108 to the volume ofthe supercritical fluid contained within the heat transfer element 107.In one embodiment, the indirect heat exchange system includes anintermediate heat transfer element 111 configured to transfer thermalenergy from the one or more heat source 108 to the intermediate heattransfer element 111. In turn, the intermediate heat transfer element111 may transfer thermal energy from the intermediate heat transferelement 111 to the volume of the supercritical fluid contained withinthe heat transfer element 107.

In one embodiment, the intermediate heat transfer element 111 mayinclude an intermediate heat transfer loop 113, and one or more heatexchangers 115, 117. In one embodiment, the intermediate heat transferloop 113 may include any working fluid known in the art suitable fortransferring thermal energy. For example, the working fluid of theintermediate heat transfer loop 113 may include, but is not limited to,a liquid salt, a liquid metal, a gas, a supercritical fluid (e.g.,supercritical CO₂) or water.

In another embodiment, the intermediate heat transfer element 111 mayinclude a first heat exchanger 115 in thermal communication with aportion of the one or more heat sources 108 and the intermediate heattransfer loop 113. In another embodiment, the indirect heat exchangesystem 111 may include a second heat exchanger 117 in thermalcommunication with the intermediate heat transfer loop 113 and the heattransfer element 107. For example, in the case where the one or moreheat sources 108 include a nuclear reactor, one or more coolant systems(e.g., primary, intermediate or ternary) of the nuclear reactor (e.g., amolten salt cooled nuclear reactor, a liquid metal cooled reactor, a gascooled reactor or and a supercritical fluid cooled reactor) may becoupled to the intermediate heat transfer loop 113 via a first exchanger115. In turn, upon transferring thermal energy from the nuclear reactorto the intermediate heat transfer loop 113 via the first heat exchanger115, the intermediate heat transfer loop 113 may transfer the nuclearreactor generated thermal energy from the intermediate transfer loop 113to the supercritical fluid contained within the heat transfer element107 via a second heat exchanger 117.

Further, as described previously herein, the heat transfer element 107of the heat transfer system 106 may intermix the supercritical fluidcontained within the heat transfer element 107 with the feedstockmaterial 105 contained within the thermochemical reaction chamber 104.In turn, upon transferring thermal energy from the nuclear reactor tothe feedstock material 105 via the intermediate heat transfer system 111and the heat transfer element 107, the thermal energy transfer system106 may re-circulate the supercritical fluid coolant via return path118.

It is noted herein that the above description of the direct and indirectcoupling between the one or more heat sources 108 and the feedstock 105is not limiting and is provided merely for illustrative purposes. It isrecognized herein that in a general sense the integration between theone or more heat sources (e.g., nuclear reactor) and the thermochemicalreaction chamber 104 may occur by transferring heat from a primary,intermediate, or ternary heat transfer system (e.g., coolant system) ofthe one or more heat sources 108 to the working fluid, such assupercritical CO₂, of the thermochemical conversion system 102. It isfurther recognized herein that this integration may be carried out usingany heat transfer systems or devices known in the art, such as, but notlimited to, one or more heat transfer circuits, one or more heat sinks,one or more heat exchangers and the like.

In one embodiment, the thermal energy transfer system 106 includes aflow control system 110. The flow control system 110 may be arranged toselectably place the supercritical fluid in thermal communication withthe volume of feedstock contained within the thermochemical reactionchamber 104. In this regard, the flow control system 110 may selectablytransfer thermal energy from the one or more heat sources 108 to thevolume of feedstock contained within thermochemical reaction chamber104. For example, the flow control system 110 may be positioned alongthe heat transfer element 107 (e.g., heat transfer loop) in order tocontrol the flow of supercritical fluid through the heat transferelement 107. In this regard, the flow control system 110 may control theflow of the supercritical fluid to the volume of feedstock 105, therebycontrolling the transfer of thermal energy to the feedstock 105.

The flow control system 110 may include any flow control system known inthe art suitable for controlling supercritical fluid flow from a firstposition to a second position. For example, the flow control system 110may include, but is not limited to, to one or more control valvesoperably coupled to the heat transfer element 107 and suitable forestablishing and stopping flow through the heat transfer element 107.For instance, the flow control system 110 may include a manuallycontrolled valve, a valve/valve actuator and the like.

In another embodiment, the flow control system 110 may couple thethermal energy from the one or more heat sources 108 to the electricalgeneration system 114. For example, the flow control system 110 mayestablish a parallel coupling of heat source 108 generated heat to aturbine electric system and the thermochemical conversion system 102. Inone embodiment, the thermochemical conversion system 102 may includemultiple batch-type reaction systems, which may receive heat from theone or more heat sources 108 (e.g., nuclear reactor). In this manner, itis possible to run multiple batch processes, concurrently orsequentially, which address overall thermal and feedstock conversionneeds. In another embodiment, heat may be transferred to one or morecontinuous thermochemical reactors while being coupled in parallel toone or more turbine electric system.

In one embodiment, the system 100 includes a feedstock supply system112. In one embodiment, the feedstock supply system 112 is operablycoupled to the thermochemical reaction chamber 104 of the thermochemicalconversion system 102. In another embodiment, the feedstock supplysystem 112 provides a volume of feedstock material 105 to the interiorof the thermochemical reaction chamber 104. The feedstock supply system112 may include any supply system known in the art suitable fortranslating a selected amount of feedstock material, such as solidmaterial, particulate material or liquid material, from one or morefeedstock sources to the interior of the thermochemical reaction chamber104. For example, the feedstock supply system 112 may include, but notlimited, to a conveyor system, a fluid transfer system and the like.

The feedstock material 105 may include any carbonaceous material knownin the art. For example, the feedstock material 105 may include, but isnot limited to, coal, biomass, mixed-source biomaterial, peat, tar,plastic, refuse, and landfill waste. For example, in the case of coal,the feedstock may include, but is not limited to, bituminous coal,sub-bituminous coal, lignite, anthracite and the like. By way of anotherexample, in the case of biomass, the feedstock may include a woodmaterial, such as, but not limited to, softwoods or hardwoods.

It is noted herein that the ability to control temperature, pressure,reaction time, pre-treatment options, and post organic-productproduction options may allow for multiple types of carbonaceousfeedstock to be utilized within the system 100. In addition, the abilityto co-utilize or switch between types of feedstock may improve theutilization of available resources and improve the overall systemeconomics. In some embodiments, it may be useful to placenon-bio-derived products into the thermochemical reaction chamber 10 forthermochemical conversion. For example, this may include the conversionof materials, such as plastics, into alternative products or fuels. Byway of another example, the thermochemical reaction chamber 104 maythermochemically process a combination of feedstock materials may be toform one or more reaction products or alternative products. Forinstance, the thermochemical reaction chamber 104 may thermochemicallyconvert a volume of feedstock consisting of a combination of plastic(s)and cellulosic material. By way of another example, the thermochemicalreaction chamber 104 thermochemically process or convert mixed sourcesof materials, or mixed wastes, such as refuse or landfill wastes, to oneor more reaction products or alternative products.

Referring again to FIGS. 1A and 1B, the thermochemical conversion system102 includes any thermochemical reaction chamber 104 suitable forcarrying out one or more thermal decomposition processes know in theart.

In one embodiment, the thermochemical reaction chamber 104 is configuredto carry out a pyrolysis reaction on the feedstock 105. In anotherembodiment, the thermochemical reaction chamber 104 includes a pyrolysischamber. In another embodiment, the thermochemical reaction chamber 104includes a non-combustion or low-combustion pyrolysis chamber. Thepyrolysis chamber of system 100 may encompass any thermochemicalreaction chamber suitable for carrying out the thermochemicaldecomposition of organic molecules in the absence of oxygen or in a lowoxygen environment.

In one embodiment, the thermochemical reaction chamber 104 includes afast pyrolysis reactor suitable for converting feedstock 105, such asbiomass, to a reaction product, such as bio-oil (e.g., bio-oil which maybe further uprated to produce liquid fuel), volatile gas or char. A fastpyrolysis reactor may include any thermochemical reaction chambercapable of carrying out a thermochemical decomposition of organicmolecules in the absence of oxygen (or in a reduced oxygen environment)within approximately two seconds. Fast pyrolysis is generally describedby Roel J. M. Westerhof et al. in “Effect of Temperature in FluidizedBed Fast Pyrolysis of Biomass: Oil Quality Assessment in Test Units,”Industrial & Engineering Chemistry Research, Volume 49 Issue 3 (2010),pp. 1160-1168, which is incorporated herein by reference in theentirety. Pyrolysis and fast pyrolysis are also generally described byAyhan Demirbas et al. in “An Overview of Biomass Pyrolysis,” EnergySources, Volume 24 Issue 3 (2002), pp. 471-482, which is incorporatedherein by reference in the entirety.

In another embodiment, the thermochemical reaction chamber 104 includesa supercritical pyrolysis reactor suitable for converting feedstock 105,such as biomass, to a reaction product, such as bio-oil (e.g., bio-oilwhich may be further uprated to produce liquid fuel), volatile gas orchar. For the purposes of the present disclosure, a ‘supercriticalpyrolysis reactor’ is interpreted to encompass any reactor, reactionvessel or reaction chamber suitable for carrying out a pyrolysisreaction of feedstock material using the thermal energy supplied from asupercritical fluid. In another embodiment, the thermochemical reactionchamber 104 may include, but is not limited to, a fluidized bed reactor.

Combustion of feedstock may be avoided, or at least reduced, byemploying an external heat source (e.g., heat source 108), such as anuclear reactor, to supply thermal energy to drive the pyrolysisreaction (or any other thermal decomposition process) of system 100.Further, as noted previously herein, the use of a supercritical fluid,such as supercritical CO₂, may drive pyrolysis in the feedstock materialwithout generating excessive temperatures commonly associated withcombustion-driven pyrolysis reactions, which commonly yield char,resulting in lighter, aromatic, hydrocarbons, which reduce theconversion efficiency of the oil product.

In one embodiment, the thermochemical reaction chamber 104 may include apyrolysis reaction chamber (e.g., fast pyrolysis reactor orsupercritical pyrolysis reactor) for thermally decomposing the feedstock105 into one or more reaction products, at a temperature between 350°and 600° C., using the thermal energy transferred from the volume ofsupercritical fluid contained within the heat transfer element 105. Forexample, the thermochemical reaction chamber 104 may include a fastpyrolysis reaction chamber for thermally decomposing the feedstock 105at a temperature between approximately 350° and 600° C. using thethermal energy transferred from a nuclear reactor via the volume ofsupercritical fluid contained within the heat transfer element 107. Byway of another example, the thermochemical reaction chamber 104 mayinclude, but is not limited to, a supercritical pyrolysis reactor forthermally decomposing the feedstock 105 at a temperature of betweenapproximately 350° and 600° C. using the thermal energy transferred froma nuclear reactor via the volume of supercritical fluid contained withinthe heat transfer element 105.

In another embodiment, the thermochemical reaction chamber 104 isconfigured to carry out a liquefaction process on the feedstock 105.Those skilled in the art will recognize that liquefaction may generallyinclude a sequence of structural and chemical processes leading to thegeneral breakdown of complex organic materials (such as carbonaceousbiomass material) to products, such as bio-oil. Liquefaction mayinclude, but is not limited to, solvolysis, depolymerization, thermaldecomposition, hydrogenolysis and/or hydrogenation. Liquefaction ofbiomass is generally described by Ralph P. Overend et al. (eds.) in“Biomass Liquefaction: An Overview,” Fundamentals of ThermochemicalBiomass Conversion, Elsevier Applied Science Publishers LTD., 1985, pp.967-1002, which is incorporated herein by reference in the entirety.

In another embodiment, the thermochemical reaction chamber 104 includesa liquefaction chamber for implementing a liquefaction process on thefeedstock 105 using the thermal energy supplied to the thermochemicalreaction chamber 104 via the supercritical fluid from heat transferelement 107. By way of example, the thermochemical reaction chamber 104may include, but is not limited to, a supercritical liquefactionreactor. For the purposes of the present disclosure, a ‘supercriticalliquefaction reactor’ is interpreted to encompass any reactor, reactionvessel or reaction chamber suitable for carrying out a liquefactionprocess on the feedstock material using the supercritical fluid.

As noted previously herein, some supercritical fluids, such assupercritical CO2, display low viscosity and surface tension, whichallow these supercritical fluids to penetrate organic materials. It isfurther noted herein that the penetration of organic materials by agiven supercritical fluid may reduce the need for converting the biomassinto fine particles for reaction, thereby reducing energy consumption inthe reaction of the feedstock material.

In one embodiment, the thermochemical reaction chamber 104 includes aliquefaction chamber for implementing a high temperature liquefactionprocess on the feedstock 105 in the presence of the supercritical fluid(e.g., supercritical CO₂). In one embodiment, the supercritical fluidneeded for the supercritical fluid liquefaction is transferred to thefeedstock 105 by intermixing the supercritical fluid with the feedstock105 in the thermochemical reaction chamber 104. The supercritical fluidsupplies both heat transfer to the feedstock material 105 and physicalinteraction with the feedstock material at the cellular level. In oneembodiment, the thermochemical reaction chamber 104 may carry out theliquefaction process on the feedstock 105 in the presence of thesupercritical fluid at a temperature in the range 300° to 500° C.

In one embodiment, the thermochemical reaction chamber 104 may carry outa liquefaction step including the deconstruction of cellulosic materialof a feedstock material (e.g., biomass feedstock material). It is notedherein that this cellulosic deconstruction provides for improved accessto inner sugars of the feedstock material, while also de-convolutinglignin and hemicellulose chains in the feedstock material. It is furthernoted herein that cellulosic breakdown of feedstock material may becarried out using the supercritical fluid supplied to the feedstockmaterial. In the case of supercritical CO₂, the CO₂ may expand thecellular structure of the feedstock material until the cells walls ofthe material are destroyed or the cellulosic material begins to rip. Inthis regard, supercritical CO₂, which is soluble in water, may diffusethrough pores in the lignocellulosic biomass and selectively react withnon-polar components of the biomass material, such as hydrocarbons. Thesudden expansion of the CO₂, which may be trapped in the pores of thelignocellulosic biomass, may then lead to the deconstruction of thebiomass. Further, this process may also lead to the deconvolution offundamental molecules, such as lignin and hemicellulosic chains in thefeedstock.

In another embodiment, the thermochemical reaction chamber 104 may carryout a liquefaction step including depolymerization. For example, thedepolymerization may lead to the breakdown of fundamental molecules,such as, but not limited to, lignin or hemicellulose in the feedstockmaterial 105 (or intermediate products from the feedstock material). Forinstance, the depolymerization-based liquefaction of system 100 maycause molecule-to-molecule breakdown or breakdown of various moleculargroups from given molecules in the feedstock (or intermediate products).

In another embodiment, the thermochemical reaction chamber 104 may carryout a liquefaction step including thermal decomposition. For example,the thermal decomposition of the feedstock (or intermediate products)may lead to fracturing across inter-molecular bonds (e.g., carbon-carbonbonds are fractured) within the molecules of the feedstock material (orintermediate products).

In another embodiment, the thermochemical reaction chamber 104 may carryout one or more extraction processes on the feedstock (or intermediateproducts) in conjunction with liquefaction. In another embodiment, anextraction chamber operably coupled to the thermochemical reactionchamber 104 may carry out one or more extraction processes on thefeedstock (or intermediate products) in conjunction with liquefaction.In one embodiment, the thermochemical reaction chamber 104 is configuredto remove additional compounds from the feedstock material prior topyrolysis. For example, the thermochemical reaction chamber 104 may beconfigured to remove at least one of oils and lipids, sugars, or otheroxygenated compounds. In another embodiment, the extracted compounds maybe collected and stored for the development of additional bio-derivedproducts.

It is noted herein that it is particularly advantageous to remove sugarsfrom the feedstock material 105. It is recognized herein that sugarscaramelize at elevated temperature and may act to block thesupercritical fluid, such as supercritical CO₂, from entering thecellulose structure of the feedstock material 105. In addition, sugarspresent in the thermochemical conversion system 102 may also act to harmdownstream catalyst beds (if any). It is noted herein that the removalof sugars aids in avoiding the formation of oxygenated compounds suchas, but not limited to, furfural, hydroxymethalfurfural, vanillin andthe like.

In one embodiment, the thermochemical conversion system 102 may extractmaterials from the feedstock 105 at temperatures below 200° C. It isnoted herein that it is beneficial to extract sugars at temperaturesbelow 200° C. as fructose, sucrose and maltose each caramelize attemperatures below approximately 180° C. In this regard, thesupercritical fluid, through the deconstruction of cellulosic materialand the sweeping away of sugars, may serve to extract sugars from thefeedstock 105 prior to the elevation of temperatures during pyrolysis.

In another embodiment, the thermochemical reaction chamber 104 may carryout a liquefaction step including hydrogenation. It is noted herein thatduring liquefaction hydrogenation may serve to heal frayed molecularbonds within the one or more reaction products, such as bio-oil, therebystabilizing the one or more reaction products.

In another embodiment, the thermochemical reaction chamber 104 isconfigured to dry the feedstock 105 to a selected dryness level prior tothermal decomposition. In another embodiment, a dryer operably coupledto the thermochemical reaction chamber 104 is configured to dry thefeedstock 105 to a selected dryness level prior to thermaldecomposition. For example, the thermochemical reaction chamber 104 (orthe dryer) may utilize the supercritical fluid to dry the feedstock 105to a selected level. For example, the thermochemical reaction chamber104 may dry the feedstock 105 to a 5.0 to 15.0% moisture content level.By way of another example, the thermochemical reaction chamber 104 maycontrol the moisture content, such that some amount of moisture remainsin the feedstock 105 material. For instance, in the case of pine wood,the thermochemical reaction chamber 104 may vary the moisture contentlevel from approximately 7.0 to 55%.

In another embodiment, the thermochemical reaction chamber 104 isconfigured to pre-heat the feedstock 105 prior to thermal decomposition.In another embodiment, a pre-heating chamber 104 operably coupled to thethermochemical reaction chamber 104 is configured to pre-heat thefeedstock 105 prior to thermal decomposition. For example, thethermochemical reaction chamber 104 (or the pre-heating chamber) maypre-heat the feedstock material to a temperature at or near thetemperature necessary for liquefaction and/or pyrolysis.

In another embodiment, the thermochemical reaction chamber 104 isconfigured to pre-treat the feedstock 105 prior to thermaldecomposition. For example, the thermochemical reaction chamber 104 maypre-hydrotreat the feedstock material with hydrogen prior toliquefaction and/or pyrolysis. For instance, pre-treating the feedstockmaterial with hydrogen may aid in removing materials such as, but notlimited to, sulfur, as well as serving to donate hydrogen to brokendangling bonds (i.e., stabilizing free radicals).

FIG. 1C illustrates a thermochemical conversion system 102 equipped withmultiple process chambers for carrying out the various steps of themulti-stage thermochemical process of system 100. In one embodiment, thethermochemical conversion system includes a dedicated dryer/pre-heater134, a liquefaction chamber 136, an extraction chamber 138 and apyrolysis chamber 140.

Applicants note that while the above description points out that in someembodiments the pyrolysis reaction chamber, liquefaction chamber, theextraction chamber, and/or the dryer/pre-heater may exist as separatechambers, this should not be interpreted as a limitation. Rather, it iscontemplated herein that two or more of the thermochemical steps mayeach be carried out in a single reaction chamber.

In one embodiment, the thermochemical reaction chamber 104 includes amulti-stage single thermochemical reaction chamber. In one embodiment,the thermal energy transfer system 102 is configured to transfermultiple portions of the supercritical fluid across multiple temperatureranges to the volume of feedstock 105 contained within the multi-stagesingle thermochemical reaction chamber 104 to perform a set ofthermochemical reaction processes on the at least a portion of thevolume of feedstock.

In another embodiment, the thermal energy transfer system 102 isconfigured to transfer a first portion of the supercritical fluid in afirst temperature range to the volume of feedstock 105 contained withinthe single thermochemical reaction chamber 104 to perform a dryingprocess on the at least a portion of the volume of feedstock.

In another embodiment, the thermal energy transfer system 102 isconfigured to transfer a second portion of the supercritical fluid in asecond temperature range to the volume of feedstock 105 contained withinthe single thermochemical reaction chamber 104 to perform a pre-heatingprocess on the at least a portion of the volume of feedstock.

In another embodiment, the thermal energy transfer system 102 isconfigured to supply a third portion of the supercritical fluid in asecond temperature range to the volume of feedstock 105 contained withinthe single thermochemical reaction chamber 104 to perform a liquefactionprocess on the at least a portion of the volume of feedstock.

In another embodiment, the thermal energy transfer system 102 isconfigured to supply a fourth portion of the supercritical fluid in afourth temperature range to the volume of feedstock 105 contained withinthe single thermochemical reaction chamber 104 to perform an extractionprocess on the at least a portion of the volume of feedstock to removeat least one oxygenated compound from the at least a portion of thefeedstock.

In another embodiment, the thermal energy transfer system 102 isconfigured to supply a fifth portion of the supercritical fluid in afifth temperature range to the volume of feedstock 105 contained withinthe single thermochemical reaction chamber 104 to perform a pyrolysisprocess on the at least a portion of the volume of feedstock

In one embodiment, the flow and temperature of the supercritical fluid(e.g., supercritical CO2) are varied spatially across the thermochemicalreaction chamber 104. For example, in order to vary flow and/ortemperature across the reaction chamber 104, multiple flows ofsupercritical fluid, each at a different temperature, may be establishedprior to entering the single reaction chamber. In this regard, in avertical reaction chamber, the flow rate and temperature at a number ofspatial locations, corresponding to the various thermochemical stages,may be varied. By way of another example, the temperature of thesupercritical fluid may be varied along the length of the thermochemicalreaction chamber 104 by flowing the supercritical fluid along the lengthof the thermochemical reaction chamber 104. For instance, a flow of lowtemperature supercritical CO₂ may be combined with a flow of CO₂ at ahigher temperature (e.g., between 70° to 150° C.) to dissolve sugars. Atanother point downstream (e.g., 1-3 meters downstream with an averageflow rate of 0.25-4 m/s), supercritical CO₂ at or above pyrolysistemperatures (e.g., above 500° C.) is mixed into the chamber. By stagingthe temperatures of the various thermochemical reaction steps accordingto length, the flow rate may be used to control reaction times.

It is further contemplated that two or more thermochemical steps, suchas pyrolysis, liquefaction and extraction, are carried out in thethermochemical chamber 104, while additional steps, such as drying andpre-heating are carried out in a dedicated chamber operably coupled tothe thermochemical reaction chamber 104.

Referring to FIGS. 1A-1E, the system 100 includes a separation unit 113,in accordance with one or more embodiments of system 100. In oneembodiment, the separator unit 119 is operably coupled to thethermochemical reaction chamber 104 and arranged to separate one or morematerials from the supercritical fluid exiting the thermochemicalreaction chamber 104. For example, the separator unit 119 may be placedin fluidic communication with an outlet of the thermochemical reactionchamber 104 and configured to separate one or more reaction products(resulting from the thermochemical decomposition of feedstock material)from the supercritical fluid exiting the thermochemical reaction chamber104.

In one embodiment, the separator unit 119 includes a solubilitycontroller. For example, the solubility controller may be configured tocontrol a solubility parameter of one or more reaction productscontained within the supercritical fluid following thermochemicalreaction of the feedstock material 105. In one embodiment, thesolubility controller may be configured to change the pressure via apressure control element, thereby controlling the solubility of thereaction products in the supercritical fluid. For example, thesupercritical fluid (e.g., supercritical CO₂) may be expanded (e.g.,expanded in expansion chamber) to a lower pressure supercritical state,a liquid state, or a gaseous states in order to remove and separationdissolved or entrained in the supercritical fluid. For instance, bio-oilor a hydrotreated product may be extracted from the volume ofsupercritical fluid by reducing the pressure of the supercritical fluid,causing the bio-oil or hydrotreated product to fall out of thesupercritical fluid. It is noted herein that it may be possible tochange the pressure of the supercritical fluid without causing the fluidto leave the supercritical state.

In another embodiment, the solubility controller may be configured tochange the temperature via a temperature control element (e.g.,heating/cooling element) of the supercritical fluid, thereby controllingthe solubility of the reaction products in the supercritical fluid. Forinstance, bio-oil or a hydrotreated product may be extracted from thevolume of supercritical fluid by changing the temperature of thesupercritical fluid, causing the bio-oil or hydrotreated product to fallout of the supercritical fluid.

In another embodiment, the solubility controller may be configured tochange the solvent concentration of the supercritical fluid, therebycontrolling the solubility of the reaction products in the supercriticalfluid.

In another embodiment, the solubility controller may control thesolubility of one or more reaction products, such as bio-oil, in thesupercritical fluid by adding or removing a polar material into thesupercritical fluid. For example, the solubility of one or more oils insupercritical carbon dioxide may be controlled by the addition/removalof one or more materials including a polar molecule. For instance, thepolar molecules may include, but are not limited to, H₂, H₂O, alcoholsand the like. By way of another example, in the case where the feedstockmaterial includes coal, the solubility of one or more oils insupercritical CO₂ may be controlled by adding/removing one or morematerials including a hydrogen donor molecule. For instance, thehydrogen donor material may include, but is not limited to, H₂, H₂O andany other hydrogen donor solvents known in the art, such as, (tetraline,tetrahydrofluoranthene (4HFL), dihydroanthacene (2HAn)).

In one embodiment, the separator unit 119 includes one or more physicalflow separators. For example, the one or more physical flow separatorsmay include one or more filters configured to separate one or morereaction products (e.g., char) from the supercritical fluid. By way ofanother example, the one or more physical flow separators may include adensity-based separation, whereby one or more reaction products areseparated from the supercritical fluid according to density.

In another embodiment, the one or more reaction products generated bythe thermochemical reaction chamber 104 may include, but is not limitedto, char, bio-oil, volatile gases and the like. In another embodiment,one or more of the reaction products from the thermochemical reactionchamber 104 are soluble in the supercritical fluid (e.g., supercriticalCO2).

In another embodiment, the system 100 includes an electrical generationsystem 114. In one embodiment, the electrical generation system 114 isplaced in fluidic communication with the thermochemical reaction chamber104. In another embodiment, the electrical generation system 114 isconfigured to receive the supercritical fluid from the thermochemicalreaction chamber 114 and generate electricity with the heatedsupercritical fluid following conversion of the feedstock 105 to one ormore reaction products. It is noted herein that the supercritical fluid(e.g., supercritical CO₂) leaving the thermochemical reaction chamber104 will have a temperature at or near the reaction temperature (e.g.,pyrolysis reaction temperature) and, therefore, may contain sensibleheat. In one embodiment, the supercritical fluid, upon exiting thethermochemical reaction chamber 104, may heat an additional workingfluid via one or more heat exchangers (not shown in FIGS. 1A-1E). Theheated additional working fluid may then drive a portion of theelectrical generation system 114, such as a rotor of a turbine, in orderto produce electricity.

In another embodiment, the supercritical fluid, upon exiting thethermochemical reaction chamber 104, may directly drive a portion of theelectrical generation system 114. For example, the supercritical fluid,upon exiting the thermochemical reaction chamber 104, may directly drivea turbine (or other machinery for the production of work) to generateelectricity. In another embodiment, one or more separation units 119, asdescribed previously herein, may separate one or more reaction productsfrom the super critical fluid exiting the chemical reaction chamber 104prior to entry into the rotating machinery of the electrical generationsystem 114.

In another embodiment, electricity produced by the electrical generationsystem 114 is utilized to augment one or more sub-systems of system 100.In one embodiment, the electrical generation system 114 is electricallycoupled to a portion of the system 100 and configured to augment the 100with at least a portion of the generated electricity. For example, theelectrical generation system 114 may be electrically coupled to acomponent of the thermochemical conversion system 102 and configured toaugment the thermochemical conversion system 102 with at least a portionof the generated electricity. For instance, electricity form theelectrical generation system 114 may be used to power one or morematerial transfer systems (e.g., feedstock supply system) of thethermochemical conversion system 102. In another instance, electricityform the electrical generation system 114 may be used to power one ormore processing systems of the thermochemical conversion system 102. Inanother instance, electricity form the electrical generation system 114may be used to power one or more heating systems (e.g., heating elementof pre-heater) used to heat material utilized or processed by thethermochemical conversion system 102. By way of another example, theelectrical generation system 114 may be electrically coupled to acomponent of the thermal energy transfer system 106 and configured toaugment the thermal energy transfer system 106 with at least a portionof the generated electricity. For instance, electricity form theelectrical generation system 114 may be used to power one or more pumpsof the thermal energy transfer system 106.

In another embodiment, electricity produced by the electrical generationsystem 114 is transferred to an external power consuming system. In oneembodiment, the electrical generation system 114 is electrically coupledto a portion of a consumer electrical grid and configured to supplyelectrical power to the electrical grid.

In another embodiment, electricity produced by the electrical generationsystem 114 is transferred to one or more operation systems of the one ormore heat sources 108. In the case where the one or more heat sources108 is a nuclear reactor, the electrical generation system 114 may becoupled to one or more operation systems of the nuclear reactor andconfigured to supply electrical power to the one or more operationsystems (e.g., control system, safety system, coolant system (e.g.,pump(s) of coolant system), security system and the like) of the nuclearreactor.

In another embodiment, the system 100 includes a hydrogen generationsystem (not shown). In one embodiment, the hydrogen generation system iselectrically coupled to an electrical output of the electricalgeneration system 114 (or any other electrical generation system ofsystem 100). For example, electricity produced by the electricalgeneration system 114 is transferred to the hydrogen generation systemand configured to generate hydrogen. In another embodiment, the hydrogengenerated via the electricity from the electrical generation system 114may then be stored and utilized for hydrotreating and/or hydrocrackingwithin system 100 (or other associated systems).

In another embodiment, the system 100 includes a quench system 120. Inone embodiment, the quenching system 120 is placed in fluidiccommunication with the chemical reaction chamber 102, as shown in FIGS.1A-1E. In this regard, the quench system 120 may receive reactionproducts from the thermochemical reaction chamber 104. In turn, heat maybe extracted from the hot thermochemical reaction chamber 104 via a heatrecovery and/or heat rejection system 126. The extraction of heat fromthe one or more reaction products may be cooled to a selected level. Itis noted herein that this quenching process may take place quickly ormay take place over several seconds. In one embodiment, the quenchingsystem 120 may cool the reaction products from a reaction temperature(e.g., temperature of approximately 350-600° for pyrolysis reactions) toa temperature suitable for maintaining bio-oil (e.g., temperaturebetween approximately 40° and 45° C.). In another embodiment, the quenchsystem 120 may cool one or more reaction products from a reactiontemperature to a temperature suitable for hydrotreating (e.g.,temperature between approximately 200° and 400° C.) and hydrocracking(e.g., temperature between approximately 400° and 450° C.).

In another embodiment, the system 100 includes a heat recovery system126. In the case of recovery, the system 126 may recover heat from thequench system (or any other appropriate sub-system of system 100) via aheat transfer loop acting to thermally couple the quench system 120 andthe heat recovery system 126. In one embodiment, the recovered heat mayserve as a recuperator or regenerator. In one embodiment, energy may berecovered after the turbine electrical generation system 114. In anotherembodiment, energy may be recovered following the thermochemical processcarried out by chamber 104. In another embodiment, the recovered energymay be used to pre-heat feedstock material prior to thermochemicalprocessing. In another embodiment, the recovered energy may be used toproduce ancillary power (e.g., mechanical power or electrical power) toone or more sub-systems of the system 100.

In another embodiment, the system 100 may be coupled to a heat rejectionsystem. In one embodiment, the heat rejection system (not shown) rejectsnuclear generated heat to ambient conditions. In this manner multipleheat rejection systems or heat utilizing systems can be coupled. It isnoted herein that this coupling may be desirable in the event the one ormore heat sources 108 (e.g., nuclear reactor) provides more thermalenergy than can be utilized by the thermochemical conversion system 102.In another embodiment, the heat rejection couple may be utilized tosmooth thermal variations on the heat source 108 side (e.g., nuclearreactor side) of the overall thermal system. In another embodiment, inthe case of a nuclear reactor based heat source, the heat rejectioncoupling may be used to guarantee a thermal path for the removal of aportion of nuclear generated heat to ambient conditions. This portion ofnuclear generated heat may be proportional or equal to the amount ofreactor decay heat the nuclear system is capable of producing, eitherimmediately after shutdown, or within a desired time after shutdown

In another embodiment, the system 100 includes a thermochemicaltreatment system 122. In one embodiment, the thermochemical treatmentsystem 122 may carry out a treatment process on one or more reactionproducts. In another embodiment, the thermochemical treatment system 122thermochemically treat the one or more reaction products following aquenching process. In one embodiment, the thermochemical treatmentsystem 122 may carry out a hydrotreatment or hydrocracking process onthe one or more reaction products. In another embodiment, the thermalenergy from the one or more heat sources 108 may drive the hydrotreatingand/or hydrocracking carried out by treatment system 122. In anotherembodiment, the hydrogen generated by system 100 during thethermochemical reaction process and subsequent processing may beutilized to hydrotreat or hydrocrack the one or more reaction products.

In another embodiment, the system 100 includes one or more storagesystems 124 for storing one or more reaction products or one or moretreated reaction products.

FIG. 1D illustrates a volatile gas separator 126 of system 100, inaccordance with one embodiment of system 100. In one embodiment, thevolatile gas separator 126 may receive a volume of reaction productsfrom the reaction chamber 104 or the quench system 120. In anotherembodiment, the volatile gas separator 126 may separate one or morevolatile gases from the remainder of the one or more reaction products.For example, the volatile gas separator 126 may separate volatile gasessuch as, but not limited to, CH₄, C₂H₄, C₂H₆, CO, CO₂, H₂, H₂O from thesolid or liquid reaction products. It is noted herein that the volatilegas separator 126 may include any volatile gas separation device orprocess known in the art. It is further recognized that these gases maybe cooled, cleaned, collected and stored for future utilization.Volatile gases may be produced in order to provide a hydrogen source forany one of the various thermochemical steps described in the presentdisclosure (e.g., hydrotreating and/or hydrocracking).

In another embodiment, the system 100 includes an uprating system 128for uprating the volatile gas from the gas separator 126 and/orproducing H₂. In one embodiment, the uprating system 128 is coupled toexternal fuel supply 130. In this regard, the external fuel supply 130may supplement the volatile gas with external fuel to generate upratedsynthesis gas (i.e., syngas) and/or H₂. For example, the external fuelsupply 130 may supply a hydrocarbon (e.g., methane, natural gas and thelike), water, steam, heat and/or electricity to the volatile gas togenerate synthesis gas and/or H₂.

In another embodiment, the uprated volatile gases may be transferred toone or more portions of the system 100 in order to enhance one or moreprocesses within the system 100. For example, the uprated volatile gasesmay transferred to one or more portions of the thermochemical conversionsystem 102 (e.g., thermochemical reaction chamber 104) in order tovolatize one or more compounds or hydrogenate one or more compoundsproduced from one or more thermochemical reactions (e.g., thermochemicalreactions taking place during liquefaction, extraction, pyrolysis andthe like). By way of another example, the uprated volatile gases may becombined with oxygen and/or air and provided to an electrical generationsystem (e.g., system 114, system 132 and the like) and combusted to addheat to a selected fluid stream prior to expansion in the electricalgeneration system (e.g., turbine of electrical generation system 114).

In another embodiment, as shown in FIG. 1E, the system 100 may includean additional electrical generation system 132. In one embodiment, theadditional electrical generation system 132 may be couple to any portionof the thermochemical conversion system 102 where sensible heat may beobtained. For example, as shown in FIG. 1E, the electrical generationsystem 132 may be coupled to the heat transfer loop between the quenchsystem 120 and heat recovery system 126.

Following are a series of flowcharts depicting implementations. For easeof understanding, the flowcharts are organized such that the initialflowcharts present implementations via an example implementation andthereafter the following flowcharts present alternate implementationsand/or expansions of the initial flowchart(s) as either sub-componentoperations or additional component operations building on one or moreearlier-presented flowcharts. Those having skill in the art willappreciate that the style of presentation utilized herein (e.g.,beginning with a presentation of a flowchart(s) presenting an exampleimplementation and thereafter providing additions to and/or furtherdetails in subsequent flowcharts) generally allows for a rapid and easyunderstanding of the various process implementations. In addition, thoseskilled in the art will further appreciate that the style ofpresentation used herein also lends itself well to modular and/orobject-oriented program design paradigms.

FIG. 2 illustrates an operational flow 200 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. In FIG. 2 and in following figures thatinclude various examples of operational flows, discussion andexplanation may be provided with respect to the above-described examplesof FIGS. 1A through 1E, and/or with respect to other examples andcontexts. However, it should be understood that the operational flowsmay be executed in a number of other environments and contexts, and/orin modified versions of FIGS. 1A through 1E. Also, although the variousoperational flows are presented in the sequence(s) illustrated, itshould be understood that the various operations may be performed inother orders than those which are illustrated, or may be performedconcurrently.

After a start operation, the operational flow 200 moves to an energygenerating operation 210. The energy generating operation 210 depictsgenerating thermal energy with at least one heat source 108. Forexample, as shown in FIGS. 1A through 1E, one or more heat sources 108may generate thermal energy. For instance, the one or more heat sources108 may include, but are not limited to, one or more nuclear reactors,such as, but not limited to, a molten salt cooled nuclear reactor, aliquid metal cooled reactor, a gas cooled reactor or a supercriticalfluid cooled reactor.

Then, feedstock providing operation 220 depicts providing a volume offeedstock. For example, as shown in FIGS. 1A through 1E, a feed stocksupply system 112 may provide a volume of feedstock 105 to one or morethermochemical reaction chambers 104. For instance, the feed stocksupply system 112 may include a solid or liquid transfer system fortransferring a supply of feedstock to the one or more thermochemicalreaction chamber 104.

Then, supercritical fluid providing operation 230 depicts providing avolume of supercritical fluid. For example, as shown in FIGS. 1A through1E, a volume of supercritical fluid may be provided and stored within aheat transfer element 107 of the thermal energy transfer system 106. Forinstance, the supercritical fluid may include, but is not limited to,supercritical carbon dioxide and supercritical water.

Then, energy transfer operation 240 depicts transferring a portion ofthe generated thermal energy to the volume of supercritical fluid. Forexample, as shown in FIGS. 1A through 1E, thermal energy generated byone or more heat sources 108 may be transferred to a supercritical fluidcontained within a heat transfer element 107 of a thermal energytransfer system 106.

Then, energy transfer operation 250 depicts transferring at least aportion of the generated thermal energy from the volume of supercriticalfluid to the volume of feedstock. For example, as shown in FIGS. 1Athrough 1E, thermal energy stored within the supercritical fluidcontained within the heat transfer element 107 of a thermal energytransfer system 106 may be transferred to the feedstock material 105contained within the thermochemical reaction chamber 104.

Then, the thermal decomposition operation 260 depicts performing athermal decomposition process on the volume of feedstock with thethermal energy transferred from the volume of supercritical fluid to thevolume of the feedstock in order to form at least one reaction product.For example, as shown in FIGS. 1A through 1E, the heat transfer element107 may supply the supercritical fluid to the feedstock materialcontained within the thermochemical reaction chamber 104. The thermalenergy stored in the supercritical fluid along with the penetration andexpansion characteristics of the supercritical fluid may thermallydecompose a portion of the feedstock 105 to form one or more reactionproducts (e.g., bio-oil).

FIG. 3 illustrates alternative embodiments of the example operationalflow 200 of FIG. 2. FIG. 3 illustrates example embodiments where theproviding operation 220 may include at least one additional operation.An Additional operation may include operation 302.

The operation 302 illustrates providing a volume of carbonaceousfeedstock. For example, as shown in FIGS. 1A through 1E, a feed stocksupply system 112 may provide a volume of carbonaceous feedstock 105 toone or more thermochemical reaction chambers 104. For instance, the feedstock supply system 112 may include a solid or liquid transfer systemfor transferring a supply of carbonaceous feedstock to the one or morethermochemical reaction chambers 104. The carbonaceous feedstock mayinclude, but is not limited to, coal, a biomass material, mixed-sourcebiomaterial, plastic, refuse and landfill waste.

FIG. 4 illustrates alternative embodiments of the example operationalflow 200 of FIG. 2. FIG. 4 illustrates example embodiments where theproviding operation 230 may include at least one additional operation.An Additional operation may include operation 402.

The operation 402 illustrates providing a volume of carbonaceousfeedstock. For example, as shown in FIGS. 1A through 1E, thermal energygenerated by one or more heat sources 108 may be transferred to a volumeof supercritical carbon dioxide contained within a heat transfer element107 of a thermal energy transfer system 106.

FIG. 5 illustrates alternative embodiments of the example operationalflow 200 of FIG. 2. FIG. 5 illustrates example embodiments where thetransferring operation 240 may include at least one additionaloperation. Additional operations may include operations 502 and/or 504.

The operation 502 illustrates directly transferring a portion of thegenerated thermal energy from the at least one heat source to the volumeof supercritical fluid. For example, as shown in FIGS. 1A through 1E,the heat transfer element 107 of the thermal energy transfer system 106may couple the working fluid of the one or more heat sources 108 (e.g.,supercritical fluid serving as coolant for nuclear reactor) directly thethermochemical reaction chamber 104.

In another embodiment, operation 504 illustrates indirectly transferringa portion of the generated thermal energy from the at least one heatsource to the volume of supercritical fluid. For example, as shown inFIGS. 1A through 1E, the system 100 may include an intermediate heattransfer system 111 configured to transfer thermal energy from theworking fluid of the one or more heat sources 108 to the heat transferfluid of the heat intermediate heat transfer element 113 (e.g., heattransfer loop) via heat exchanger 115. In turn, the intermediate thermalenergy transfer system 113 is arranged to transfer thermal energy fromthe intermediate heat transfer element 113 to the supercritical workingfluid of the thermochemical conversion system via heat exchanger 113.

FIG. 6 illustrates alternative embodiments of the example operationalflow 200 of FIG. 2. FIG. 6 illustrates example embodiments where thetransferring operation 250 may include at least one additionaloperation. An Additional operation may include operation 602.

The operation 602 illustrates transferring at least a portion of thegenerated thermal energy from the volume of supercritical fluid to thevolume of feedstock by intermixing at least a portion of the volume ofsupercritical fluid with at least a portion of the volume of feedstock.For example, as shown in FIGS. 1A through 1E, the heat transfer element107 may flow the supercritical fluid directly into the interior of thethermochemical reaction chamber 104 in order to intermix thesupercritical fluid with the feedstock material 105 disposed within thereaction chamber 105, thereby transferring a portion of the thermalenergy stored within the supercritical fluid, such as supercriticalcarbon dioxide, to the volume of feedstock.

FIG. 7 illustrates alternative embodiments of the example operationalflow 200 of FIG. 2. FIG. 7 illustrates example embodiments where thethermal decomposition operation 260 may include at least one additionaloperation. Additional operations may include operations 702, 704 and/or706.

The operation 702 illustrates performing a pyrolysis reaction process onthe volume of feedstock with the thermal energy transferred from thevolume of supercritical fluid to the volume of the feedstock in order toform at least one reaction product. For example, as shown in FIGS. 1Athrough 1E, the thermochemical reaction chamber 104 may include apyrolysis chamber in thermal communication with the supercritical fluidcontained in the heat transfer element 107. Further, the pyrolysischamber may carry out a pyrolysis process on the feedstock 105 utilizingthe thermal energy supplied to the pyrolysis chamber with thesupercritical fluid.

In another embodiment, operation 704 illustrates performing a fastpyrolysis reaction process at a temperature between 350° and 600° C. onthe volume of feedstock with the thermal energy transferred from thevolume of supercritical fluid to the volume of the feedstock in order toform at least one reaction product. For example, as shown in FIGS. 1Athrough 1E, the thermochemical reaction chamber 104 may include a fastpyrolysis chamber in thermal communication with the supercritical fluidhaving a temperature between 350° and 600° C. contained in the heattransfer element 107. Further, the pyrolysis chamber may carry out afast pyrolysis process on the feedstock 105 utilizing the thermal energysupplied to the fast pyrolysis chamber with the supercritical fluid.

In another embodiment, the operation 706 illustrates performing aliquefaction process on the volume of feedstock with the thermal energytransferred from the volume of supercritical fluid to the volume of thefeedstock in order to form at least one reaction product. For example,as shown in FIGS. 1A through 1E, the thermochemical reaction chamber 104may include a liquefaction chamber in thermal communication with thesupercritical fluid contained in the heat transfer element 107. Further,the liquefaction chamber may carry out a liquefaction process on thefeedstock 105 utilizing the thermal energy supplied to the liquefactionchamber with the supercritical fluid.

FIG. 8 illustrates an operational flow 800 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 8 illustrates an exampleembodiment where the example operational flow 800 of FIG. 8 may includeat least one additional operation. Additional operations may includeseparating operations 810, 812 and/or 814.

The operation 810 illustrates separating the at least one reactionproduct from the supercritical fluid following the at least one thermaldecomposition process. For example, as shown in FIGS. 1A through 1E, thesystem 100 may include a separator unit 119 coupled to thethermochemical reaction chamber and configured to separate the one ormore reaction products (e.g., bio-oil) from the supercritical fluid(e.g., supercritical carbon dioxide) following the thermal decompositionprocess.

In another embodiment, the operation 812 illustrates separating the atleast one reaction product from the supercritical fluid following the atleast one thermal decomposition process by controlling a solubilityparameter of the at least one product following the at least onethermochemical decomposition process. For example, as shown in FIGS. 1Athrough 1E, the system 100 may include a separator unit 119 coupled tothe thermochemical reaction chamber and configured to separate the oneor more reaction products (e.g., bio-oil) from the supercritical fluid(e.g., supercritical carbon dioxide) following the thermal decompositionprocess by controlling a solubility parameter of one or more reactionproducts. For instance, the separator unit 119 may control a solubilityparameter by controlling the pressure of the supercritical fluid.

In another embodiment, the operation 814 illustrates separating the atleast one reaction product from the supercritical fluid following the atleast one thermal decomposition process via a physical flow separator.For example, as shown in FIGS. 1A through 1E, the system 100 may includea separator unit 119 coupled to the thermochemical reaction chamber andconfigured to separate the one or more reaction products (e.g., bio-oil)from the supercritical fluid (e.g., supercritical carbon dioxide)following the thermal decomposition process via a physical flowseparator. For instance, the physical flow separator may include adensity-based separator unit.

FIG. 9 illustrates an operational flow 900 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 9 illustrates an exampleembodiment where the example operational flow 900 of FIG. 9 may includeat least one additional operation. An additional operation may includedrying operation 910.

The operation 910 illustrates prior to performing a thermaldecomposition process drying the at least a portion of the feedstock.For example, as shown in FIGS. 1A through 1E, the system 100 may includea dryer 134 for drying (e.g., drying to a moisture level of 5-15%) thefeedstock material 105 prior to the thermal decomposition process beingcarried out by the thermochemical reaction chamber 104.

FIG. 10 illustrates an operational flow 1000 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 10 illustrates an exampleembodiment where the example operational flow 1000 of FIG. 10 mayinclude at least one additional operation. An additional operation mayinclude pre-heating operation 1010.

The operation 1010 illustrates prior to performing a thermaldecomposition process pre-heating the at least a portion of thefeedstock. For example, as shown in FIGS. 1A through 1E, the system 100may include a pre-heater for pre-heating the feedstock material 105 to atemperature at or near the reaction temperature required by thethermochemical reaction chamber 104 prior to the thermal decompositionprocess being carried out by the thermochemical reaction chamber 104.

FIG. 11 illustrates an operational flow 1100 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 11 illustrates an exampleembodiment where the example operational flow 1100 of FIG. 11 mayinclude at least one additional operation. An additional operation mayinclude pre-treating operation 1110.

The operation 1110 illustrates prior to performing a thermaldecomposition process pre-treating the at least a portion of thefeedstock. For example, as shown in FIGS. 1A through 1E, the system 100may include a pre-treater for pre-treating the feedstock material 105prior to the thermal decomposition process being carried out by thethermochemical reaction chamber 104. For instance, a pre-treater (ortreatment system 122) may pre-hydrotreat the feedstock material prior tothe thermal decomposition process being carried out by thethermochemical reaction chamber 104.

FIG. 12 illustrates an operational flow 1200 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 12 illustrates an exampleembodiment where the example operational flow 1200 of FIG. 12 mayinclude at least one additional operation. Additional operations mayinclude extracting operations 1210 and/or 1211.

The operation 1210 illustrates extracting at least one material from theat least a portion of the feedstock. For example, as shown in FIGS. 1Athrough 1E, the thermochemical reaction chamber 104 is configured toremove additional compounds from the feedstock material prior topyrolysis utilizing the supercritical fluid to carry away the materials.

The operation 1212 illustrates extracting at least one oxygenatedcompound from the at least a portion of the feedstock. For example, asshown in FIGS. 1A through 1E, the thermochemical reaction chamber 104may be configured to remove at least one of oils and lipids, sugars, orother oxygenated compounds.

FIG. 13A illustrates an operational flow 1300 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 13A illustrates an exampleembodiment where the example operational flow 1300 of FIG. 13A mayinclude at least one additional operation. Additional operations mayinclude operations 1310 and/or 1320.

The operation 1310 illustrates receiving the supercritical fluidfollowing the thermochemical decomposition process. For example, asshown in FIGS. 1A through 1E, an electrical generation system 114 mayreceive the supercritical fluid from an outlet of the thermochemicalreaction chamber 104 following the thermal decomposition process.

The operation 1312 illustrates generating electricity using the receivedsupercritical fluid. For example, as shown in FIGS. 1A through 1E, theelectrical generation system 114 may generate electricity utilizing thesupercritical fluid. For instance, supercritical fluid may drive aturbine of the electrical generation system 114 in order to generateelectricity.

FIG. 13B illustrates additional embodiments of the example operationalflow 1300 of FIG. 13A. FIG. 13B illustrates an example embodiment wherethe example operational flow 1300 of FIG. 13B may include at least oneadditional operation. An additional operation may include operations1330.

The operation 1330 illustrates generating hydrogen with the generatedelectricity. For example, as shown in FIGS. 1A through 1E, a hydrogengeneration unit may be coupled to the electrical output of theelectrical generation system 114. In this regard, electricity from theelectrical generation system 114 may drive the hydrogen generation unitin order to generate hydrogen.

FIG. 14 illustrates an operational flow 1400 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 14 illustrates an exampleembodiment where the example operational flow 1400 of FIG. 14 mayinclude at least one additional operation. An additional operation mayinclude operation 1410.

The operation 1410 illustrates performing at least one of ahydrotreating process and a hydrocracking process on the at least onereaction product. For example, as shown in FIGS. 1A through 1E, thetreatment system 122 may perform a hydrotreating process or ahydrocracking process on one or more reaction products exiting thethermochemical reaction chamber 104.

FIG. 15A illustrates an operational flow 1500 representing exampleoperations related to performing thermochemical conversion of afeedstock to a reaction product. FIG. 15A illustrates an exampleembodiment where the example operational flow 1500 of FIG. 15A mayinclude at least one additional operation. An additional operation mayinclude operation 1510.

The operation 1510 illustrates quenching the at least one reactionproduct following the thermal decomposition process. For example, asshown in FIGS. 1A through 1E, the quench system 120 may quench one ormore reaction products after the one or more reaction products exit thethermochemical reaction chamber 104.

FIG. 15B illustrates additional embodiments of the example operationalflow 1500 of FIG. 15A. FIG. 15B illustrates an example embodiment wherethe example operational flow 1500 of FIG. 15B may include at least oneadditional operation. An additional operation may include operation1520.

The operation 1520 illustrates recovering heat from the at least onereaction product. For example, as shown in FIGS. 1A through 1E, a heatrecovery system 126 may be coupled to the quench system 120 andconfigured to recover heat from the quenched one or more reactionproducts via a heat transfer loop.

FIG. 15C illustrates additional embodiments of the example operationalflow 1500 of FIG. 15A. FIG. 15C illustrates an example embodiment wherethe example operational flow 1500 of FIG. 15C may include at least oneadditional operation. An additional operation may include operation1530.

The operation 1530 illustrates rejecting heating from the at least onereaction product. For example, as shown in FIGS. 1A through 1E, a heatrejection system may be thermally coupled to the thermochemicalconversion system 102 and configured to reject heat from the one or morereaction products or the supercritical fluid. For instance, the heatrejection system may be couple to a heat sink and configured to transfersurplus thermal energy stored in the one or more reaction products orthe supercritical fluid to the heat sink.

FIG. 15D illustrates additional embodiments of the example operationalflow 1500 of FIG. 15A. FIG. 15D illustrates an example embodiment wherethe example operational flow 1500 of FIG. 15D may include at least oneadditional operation. An additional operation may include operation1540.

The operation 1540 illustrates separating at least one volatile gas fromthe at least one reaction product. For example, as shown in FIGS. 1Athrough 1E, a gas separator 126 may receive one or more reactionproducts and separate one or more volatile gas reaction products fromnon-volatile gas products.

FIG. 15E illustrates additional embodiments of the example operationalflow 1500 of FIG. 15A. FIG. 15E illustrates an example embodiment wherethe example operational flow 1500 of FIG. 15E may include at least oneadditional operation. An additional operation may include operation1550.

The operation 1550 illustrates producing diatomic hydrogen using the atleast one volatile gas. For example, as shown in FIGS. 1A through 1E,the system 100 may include an uprating system 128. For instance, theuprating system 128 may receive one or more volatile gas reactionproducts from the gas separator 126 and process the volatile gasreaction products with one or more fuels (e.g., natural gas, electricityand/or water) from an external fuel supply 130. Then, the upratingsystem 128 may combine the volatile gas reaction products with theexternal fuel to generate synthesis gas or H₂.

Those having skill in the art will recognize that the state of the arthas progressed to the point where there is little distinction leftbetween hardware, software, and/or firmware implementations of aspectsof systems; the use of hardware, software, and/or firmware is generally(but not always, in that in certain contexts the choice between hardwareand software can become significant) a design choice representing costvs. efficiency tradeoffs. Those having skill in the art will appreciatethat there are various vehicles by which processes and/or systems and/orother technologies described herein can be effected (e.g., hardware,software, and/or firmware), and that the preferred vehicle will varywith the context in which the processes and/or systems and/or othertechnologies are deployed. For example, if an implementer determinesthat speed and accuracy are paramount, the implementer may opt for amainly hardware and/or firmware vehicle; alternatively, if flexibilityis paramount, the implementer may opt for a mainly softwareimplementation; or, yet again alternatively, the implementer may opt forsome combination of hardware, software, and/or firmware. Hence, thereare several possible vehicles by which the processes and/or devicesand/or other technologies described herein may be effected, none ofwhich is inherently superior to the other in that any vehicle to beutilized is a choice dependent upon the context in which the vehiclewill be deployed and the specific concerns (e.g., speed, flexibility, orpredictability) of the implementer, any of which may vary. Those skilledin the art will recognize that optical aspects of implementations willtypically employ optically-oriented hardware, software, and or firmware.

In some implementations described herein, logic and similarimplementations may include software or other control structures.Electronic circuitry, for example, may have one or more paths ofelectrical current constructed and arranged to implement variousfunctions as described herein. In some implementations, one or moremedia may be configured to bear a device-detectable implementation whensuch media hold or transmit device-detectable instructions operable toperform as described herein. In some variants, for example,implementations may include an update or modification of existingsoftware or firmware, or of gate arrays or programmable hardware, suchas by performing a reception of or a transmission of one or moreinstructions in relation to one or more operations described herein.Alternatively or additionally, in some variants, an implementation mayinclude special-purpose hardware, software, firmware components, and/orgeneral-purpose components executing or otherwise invokingspecial-purpose components. Specifications or other implementations maybe transmitted by one or more instances of tangible transmission mediaas described herein, optionally by packet transmission or otherwise bypassing through distributed media at various times.

Alternatively or additionally, implementations may include executing aspecial-purpose instruction sequence or invoking circuitry for enabling,triggering, coordinating, requesting, or otherwise causing one or moreoccurrences of virtually any functional operations described herein. Insome variants, operational or other logical descriptions herein may beexpressed as source code and compiled or otherwise invoked as anexecutable instruction sequence. In some contexts, for example,implementations may be provided, in whole or in part, by source code,such as C++, or other code sequences. In other implementations, sourceor other code implementation, using commercially available and/ortechniques in the art, may be compiled//implemented/translated/convertedinto a high-level descriptor language (e.g., initially implementingdescribed technologies in C or C++ programming language and thereafterconverting the programming language implementation into alogic-synthesizable language implementation, a hardware descriptionlanguage implementation, a hardware design simulation implementation,and/or other such similar mode(s) of expression). For example, some orall of a logical expression (e.g., computer programming languageimplementation) may be manifested as a Verilog-type hardware description(e.g., via Hardware Description Language (HDL) and/or Very High SpeedIntegrated Circuit Hardware Descriptor Language (VHDL)) or othercircuitry model which may then be used to create a physicalimplementation having hardware (e.g., an Application Specific IntegratedCircuit). Those skilled in the art will recognize how to obtain,configure, and optimize suitable transmission or computational elements,material supplies, actuators, or other structures in light of theseteachings.

The foregoing detailed description has set forth various embodiments ofthe devices and/or processes via the use of block diagrams, flowcharts,and/or examples. Insofar as such block diagrams, flowcharts, and/orexamples contain one or more functions and/or operations, it will beunderstood by those within the art that each function and/or operationwithin such block diagrams, flowcharts, or examples can be implemented,individually and/or collectively, by a wide range of hardware, software,firmware, or virtually any combination thereof. In one embodiment,several portions of the subject matter described herein may beimplemented via Application Specific Integrated Circuits (ASICs), FieldProgrammable Gate Arrays (FPGAs), digital signal processors (DSPs), orother integrated formats. However, those skilled in the art willrecognize that some aspects of the embodiments disclosed herein, inwhole or in part, can be equivalently implemented in integratedcircuits, as one or more computer programs running on one or morecomputers (e.g., as one or more programs running on one or more computersystems), as one or more programs running on one or more processors(e.g., as one or more programs running on one or more microprocessors),as firmware, or as virtually any combination thereof, and that designingthe circuitry and/or writing the code for the software and or firmwarewould be well within the skill of one of skill in the art in light ofthis disclosure. In addition, those skilled in the art will appreciatethat the mechanisms of the subject matter described herein are capableof being distributed as a program product in a variety of forms, andthat an illustrative embodiment of the subject matter described hereinapplies regardless of the particular type of signal bearing medium usedto actually carry out the distribution. Examples of a signal bearingmedium include, but are not limited to, the following: a recordable typemedium such as a floppy disk, a hard disk drive, a Compact Disc (CD), aDigital Video Disk (DVD), a digital tape, a computer memory, etc.; and atransmission type medium such as a digital and/or an analogcommunication medium (e.g., a fiber optic cable, a waveguide, a wiredcommunications link, a wireless communication link (e.g., transmitter,receiver, transmission logic, reception logic, etc.), etc.).

In a general sense, those skilled in the art will recognize that thevarious embodiments described herein can be implemented, individuallyand/or collectively, by various types of electro-mechanical systemshaving a wide range of electrical components such as hardware, software,firmware, and/or virtually any combination thereof; and a wide range ofcomponents that may impart mechanical force or motion such as rigidbodies, spring or torsional bodies, hydraulics, electro-magneticallyactuated devices, and/or virtually any combination thereof.Consequently, as used herein “electro-mechanical system” includes, butis not limited to, electrical circuitry operably coupled with atransducer (e.g., an actuator, a motor, a piezoelectric crystal, a MicroElectro Mechanical System (MEMS), etc.), electrical circuitry having atleast one discrete electrical circuit, electrical circuitry having atleast one integrated circuit, electrical circuitry having at least oneapplication specific integrated circuit, electrical circuitry forming ageneral purpose computing device configured by a computer program (e.g.,a general purpose computer configured by a computer program which atleast partially carries out processes and/or devices described herein,or a microprocessor configured by a computer program which at leastpartially carries out processes and/or devices described herein),electrical circuitry forming a memory device (e.g., forms of memory(e.g., random access, flash, read only, etc.)), electrical circuitryforming a communications device (e.g., a modem, communications switch,optical-electrical equipment, etc.), and/or any non-electrical analogthereto, such as optical or other analogs. Those skilled in the art willalso appreciate that examples of electro-mechanical systems include butare not limited to a variety of consumer electronics systems, medicaldevices, as well as other systems such as motorized transport systems,factory automation systems, security systems, and/orcommunication/computing systems. Those skilled in the art will recognizethat electro-mechanical as used herein is not necessarily limited to asystem that has both electrical and mechanical actuation except ascontext may dictate otherwise.

In a general sense, those skilled in the art will recognize that thevarious aspects described herein which can be implemented, individuallyand/or collectively, by a wide range of hardware, software, firmware,and/or any combination thereof can be viewed as being composed ofvarious types of “electrical circuitry.” Consequently, as used herein“electrical circuitry” includes, but is not limited to, electricalcircuitry having at least one discrete electrical circuit, electricalcircuitry having at least one integrated circuit, electrical circuitryhaving at least one application specific integrated circuit, electricalcircuitry forming a general purpose computing device configured by acomputer program (e.g., a general purpose computer configured by acomputer program which at least partially carries out processes and/ordevices described herein, or a microprocessor configured by a computerprogram which at least partially carries out processes and/or devicesdescribed herein), electrical circuitry forming a memory device (e.g.,forms of memory (e.g., random access, flash, read only, etc.)), and/orelectrical circuitry forming a communications device (e.g., a modem,communications switch, optical-electrical equipment, etc.). Those havingskill in the art will recognize that the subject matter described hereinmay be implemented in an analog or digital fashion or some combinationthereof.

Those skilled in the art will recognize that at least a portion of thedevices and/or processes described herein can be integrated into a dataprocessing system. Those having skill in the art will recognize that adata processing system generally includes one or more of a system unithousing, a video display device, memory such as volatile or non-volatilememory, processors such as microprocessors or digital signal processors,computational entities such as operating systems, drivers, graphicaluser interfaces, and applications programs, one or more interactiondevices (e.g., a touch pad, a touch screen, an antenna, etc.), and/orcontrol systems including feedback loops and control motors (e.g.,feedback for sensing position and/or velocity; control motors for movingand/or adjusting components and/or quantities). A data processing systemmay be implemented utilizing suitable commercially available components,such as those typically found in data computing/communication and/ornetwork computing/communication systems.

One skilled in the art will recognize that the herein describedcomponents (e.g., operations), devices, objects, and the discussionaccompanying them are used as examples for the sake of conceptualclarity and that various configuration modifications are contemplated.Consequently, as used herein, the specific exemplars set forth and theaccompanying discussion are intended to be representative of their moregeneral classes. In general, use of any specific exemplar is intended tobe representative of its class, and the non-inclusion of specificcomponents (e.g., operations), devices, and objects should not be takenlimiting.

Although a user is shown/described herein as a single illustratedfigure, those skilled in the art will appreciate that the user may berepresentative of a human user, a robotic user (e.g., computationalentity), and/or substantially any combination thereof (e.g., a user maybe assisted by one or more robotic agents) unless context dictatesotherwise. Those skilled in the art will appreciate that, in general,the same may be said of “sender” and/or other entity-oriented terms assuch terms are used herein unless context dictates otherwise.

With respect to the use of substantially any plural and/or singularterms herein, those having skill in the art can translate from theplural to the singular and/or from the singular to the plural as isappropriate to the context and/or application. The varioussingular/plural permutations are not expressly set forth herein for sakeof clarity.

The herein described subject matter sometimes illustrates differentcomponents contained within, or connected with, different othercomponents. It is to be understood that such depicted architectures aremerely exemplary, and that in fact many other architectures may beimplemented which achieve the same functionality. In a conceptual sense,any arrangement of components to achieve the same functionality iseffectively “associated” such that the desired functionality isachieved. Hence, any two components herein combined to achieve aparticular functionality can be seen as “associated with” each othersuch that the desired functionality is achieved, irrespective ofarchitectures or intermedial components. Likewise, any two components soassociated can also be viewed as being “operably connected”, or“operably coupled,” to each other to achieve the desired functionality,and any two components capable of being so associated can also be viewedas being “operably couplable,” to each other to achieve the desiredfunctionality. Specific examples of operably couplable include but arenot limited to physically mateable and/or physically interactingcomponents, and/or wirelessly interactable, and/or wirelesslyinteracting components, and/or logically interacting, and/or logicallyinteractable components.

In some instances, one or more components may be referred to herein as“configured to,” “configurable to,” “operable/operative to,”“adapted/adaptable,” “able to,” “conformable/conformed to,” etc. Thoseskilled in the art will recognize that such terms (e.g., “configuredto”) can generally encompass active-state components and/orinactive-state components and/or standby-state components, unlesscontext requires otherwise.

While particular aspects of the present subject matter described hereinhave been shown and described, it will be apparent to those skilled inthe art that, based upon the teachings herein, changes and modificationsmay be made without departing from the subject matter described hereinand its broader aspects and, therefore, the appended claims are toencompass within their scope all such changes and modifications as arewithin the true spirit and scope of the subject matter described herein.It will be understood by those within the art that, in general, termsused herein, and especially in the appended claims (e.g., bodies of theappended claims) are generally intended as “open” terms (e.g., the term“including” should be interpreted as “including but not limited to,” theterm “having” should be interpreted as “having at least,” the term“includes” should be interpreted as “includes but is not limited to,”etc.). It will be further understood by those within the art that if aspecific number of an introduced claim recitation is intended, such anintent will be explicitly recited in the claim, and in the absence ofsuch recitation no such intent is present. For example, as an aid tounderstanding, the following appended claims may contain usage of theintroductory phrases “at least one” and “one or more” to introduce claimrecitations. However, the use of such phrases should not be construed toimply that the introduction of a claim recitation by the indefinitearticles “a” or “an” limits any particular claim containing suchintroduced claim recitation to claims containing only one suchrecitation, even when the same claim includes the introductory phrases“one or more” or “at least one” and indefinite articles such as “a” or“an” (e.g., “a” and/or “an” should typically be interpreted to mean “atleast one” or “one or more”); the same holds true for the use ofdefinite articles used to introduce claim recitations. In addition, evenif a specific number of an introduced claim recitation is explicitlyrecited, those skilled in the art will recognize that such recitationshould typically be interpreted to mean at least the recited number(e.g., the bare recitation of “two recitations,” without othermodifiers, typically means at least two recitations, or two or morerecitations). Furthermore, in those instances where a conventionanalogous to “at least one of A, B, and C, etc.” is used, in generalsuch a construction is intended in the sense one having skill in the artwould understand the convention (e.g., “a system having at least one ofA, B, and C” would include but not be limited to systems that have Aalone, B alone, C alone, A and B together, A and C together, B and Ctogether, and/or A, B, and C together, etc.). In those instances where aconvention analogous to “at least one of A, B, or C, etc.” is used, ingeneral such a construction is intended in the sense one having skill inthe art would understand the convention (e.g., “a system having at leastone of A, B, or C” would include but not be limited to systems that haveA alone, B alone, C alone, A and B together, A and C together, B and Ctogether, and/or A, B, and C together, etc.). It will be furtherunderstood by those within the art that typically a disjunctive wordand/or phrase presenting two or more alternative terms, whether in thedescription, claims, or drawings, should be understood to contemplatethe possibilities of including one of the terms, either of the terms, orboth terms unless context dictates otherwise. For example, the phrase “Aor B” will be typically understood to include the possibilities of “A”or “B” or “A and B.

With respect to the appended claims, those skilled in the art willappreciate that recited operations therein may generally be performed inany order. Also, although various operational flows are presented in asequence(s), it should be understood that the various operations may beperformed in other orders than those which are illustrated, or may beperformed concurrently. Examples of such alternate orderings may includeoverlapping, interleaved, interrupted, reordered, incremental,preparatory, supplemental, simultaneous, reverse, or other variantorderings, unless context dictates otherwise. Furthermore, terms like“responsive to,” “related to,” or other past-tense adjectives aregenerally not intended to exclude such variants, unless context dictatesotherwise.

The invention claimed is:
 1. An apparatus comprising: a thermochemicalconversion system including at least one multi-stage singlethermochemical reaction chamber containing a volume of feedstock in areduced oxygen environment; and a thermal energy transfer systemincluding a heat transfer element containing a volume of supercriticalcarbon dioxide in thermal communication with at least one heat source,the thermal energy transfer system including a flow control systemconfigured to selectably place the volume of supercritical carbondioxide in thermal communication with at least a portion of the volumeof feedstock, wherein the at least one multi-stage single thermochemicalreaction chamber is configured to thermochemically convert at least aportion of the feedstock to at least one reaction product with thethermal energy transferred from the supercritical fluid, wherein theflow control system is programmed to transfer multiple portions of thesupercritical carbon dioxide across multiple temperature ranges to thevolume of feedstock contained within the multi-stage singlethermochemical reaction chamber to perform a set of thermochemicalreaction processes on the at least a portion of the volume of feedstock.2. The apparatus of claim 1, wherein the at least one thermochemicalreaction chamber is configured to selectably intermix the supercriticalcarbon dioxide with the volume of feedstock contained within the atleast one thermochemical reaction chamber in order to selectablytransfer thermal energy from the at least one heat source to the atleast a portion of the volume of feedstock.
 3. The apparatus of claim 1,wherein the thermal energy transfer system includes: a direct heatexchange system configured to transfer thermal energy directly from theat least one heat source to the volume of the supercritical carbondioxide of the heat transfer element.
 4. The apparatus of claim 1,wherein the thermal energy transfer system includes: an indirect heatexchange system including an intermediate heat transfer elementconfigured to transfer thermal energy from the at least one heat sourceto the intermediate heat transfer element, wherein the intermediate heattransfer element is further configured to transfer thermal energy fromthe intermediate heat transfer element to the volume of thesupercritical carbon dioxide.
 5. The apparatus of claim 1, wherein thethermal energy transfer flow control system is configured to transfer afirst portion of the supercritical carbon dioxide in a first temperaturerange to the volume of feedstock contained within the singlethermochemical reaction chamber to perform a drying process on the atleast a portion of the volume of feedstock.
 6. The apparatus of claim 1,wherein the thermal energy transfer flow control system is configured totransfer a second portion of the supercritical carbon dioxide in asecond temperature range, different from the first temperature range, tothe volume of feedstock contained within the single thermochemicalreaction chamber to perform a preheating process on the at least aportion of the volume of feedstock.
 7. The apparatus of claim 1, whereinthe thermal energy transfer flow control system is configured to supplya third portion of the supercritical carbon dioxide in a thirdtemperature range, different from the first or second temperatureranges, to the volume of feedstock contained within the singlethermochemical reaction chamber to perform a liquefaction process on theat least a portion of the volume of feedstock.
 8. The apparatus of claim1, wherein the thermal energy transfer flow control system is configuredto supply a fourth portion of the supercritical carbon dioxide in afourth temperature range, different from the first, second, or thirdtemperature ranges, to the volume of feedstock contained within thesingle thermochemical reaction chamber to perform an extraction processon the at least a portion of the volume of feedstock to remove at leastone oxygenated compound from the at least a portion of the feedstock. 9.The apparatus of claim 1, wherein the thermal energy transfer flowcontrol system is configured to supply a fifth portion of thesupercritical carbon dioxide in a fifth temperature range, differentfrom the first, second, third, or fourth temperature ranges, to thevolume of feedstock contained within the single thermochemical reactionchamber to perform a pyrolysis process on the at least a portion of thevolume of feedstock.
 10. The apparatus of claim 1, wherein the at leastone thermochemical reaction chamber includes: at least one pyrolysisreaction chamber.
 11. The apparatus of claim 10, wherein the at leastone pyrolysis reaction chamber includes: at least one fast pyrolysisreaction.
 12. The apparatus of claim 1, wherein the thermochemicalconversion system is a multi-stage thermochemical conversion systemincluding at least one pyrolysis chamber and at least one additionaltreatment chamber.
 13. The apparatus of claim 12, wherein the at leastone additional treatment chamber includes: at least one of a feedstockdryer, a pre-heater, a pre-hydrotreating chamber, a liquefaction chamberand an extraction chamber.
 14. The apparatus of claim 1, furthercomprising: a separator unit operably coupled to the at least onethermochemical reaction chamber and configured to separate at least onematerial from the supercritical carbon dioxide exiting the at leastthermochemical reaction chamber.
 15. The apparatus of claim 1, whereinthe feedstock includes: a carbonaceous material.
 16. The apparatus ofclaim 15, wherein the carbonaceous material includes: at least one ofcoal, biomass, mixed-source biomaterial, plastic, refuse, and landfillwaste.
 17. The apparatus of claim 1, wherein the supercritical carbondioxide includes: at least one of supercritical carbon dioxide andsupercritical water.
 18. The apparatus of claim 1, wherein the at leastone heat source includes: at least one nuclear reactor.
 19. Theapparatus of claim 1, wherein the at least one thermochemical reactionchamber of the thermochemical conversion system includes: at least oneof a fluidized bed reactor, a supercritical liquefaction reactor and asupercritical pyrolysis reactor.
 20. The apparatus of claim 1, furthercomprising: an electrical generation system in fluidic communicationwith the at least one thermochemical reaction chamber and configured toreceive the supercritical carbon dioxide from the thermochemicalreaction chamber and generate electricity with the supercritical carbondioxide following conversion of at least a portion of the feedstock tothe at least one reaction product.
 21. The apparatus of claim 20,wherein the electrical generation system is electrically coupled to aportion of at least one of the thermochemical conversion system and thethermal energy transfer system and configured to augment thethermochemical conversion system with at least a portion of thegenerated electricity.
 22. The apparatus of claim 20, furthercomprising: a hydrogen generation system coupled to the electricaloutput of the electrical generation system.
 23. The apparatus of claim1, further comprising: a quenching system in fluidic communication withthe at least one chemical reaction chamber.
 24. The apparatus of claim1, further comprising: a treatment system configured to generate atleast one refined product by treating the at least one reaction product.25. The apparatus of claim 1, further comprising: a volatile gasseparator configured to separate at least one volatile gas from the atleast one reaction product.
 26. The apparatus of claim 25, furthercomprising: an uprating system configured to produce diatomic hydrogenusing the at least one volatile gas from the volatile gas separator.